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Publication numberUS2880164 A
Publication typeGrant
Publication dateMar 31, 1959
Filing dateDec 23, 1954
Priority dateDec 23, 1954
Publication numberUS 2880164 A, US 2880164A, US-A-2880164, US2880164 A, US2880164A
InventorsKemeth Viland Clare
Original AssigneeTidewater Oil Company
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Manufacture of anti-knock gasoline
US 2880164 A
Abstract  available in
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Claims  available in
Description  (OCR text may contain errors)

United States Patent I arson MANUFACTURE or ANTI-KNOCK GASOLINE Clare Kenneth Vlland, Martinez, Calif, asslgnor to Tide I This invention relates to the catalytic reforming of naphtha fractions to produce gasoline constituents of high anti-knock quality. More particularly, it relates to a combination of catalytic reforming and separation processes whereby a greater yield of high quality product is obtained than can be achieved by catalytic reforming alone.

Progress in the automotive industry has resulted in the development of gasoline engines of higher and higher compression pressures, requiring gasoline fuels with'correspondingly higher anti-knock properties or "octane rating. To meet this demand, the petroleum industry has developed various processes for producing gasoline of increased octane rating. One of the more efficient of such processes is catalytic reforming wherein low-octane naphtha is contacted in the vapor-phase with suitable catalyst at temperatures above 800 F.', in the presence of substantial volumes of hydrogen. A common type of catalyst used for catalytic reforming is platinum supported on a carrier of alumina and/or silica. Several such platinum catalysts are marketed which will produce good yields of 85 to 90 research octane number (ASTM Method D908-53) reformate under operating conditions sufiiciently mild that the catalyst can be used for extended periods of time without regeneration to'remove carbon formed by undesirable cracking reactions.

More recent developments in the, automotive industry produced from other refining processes such as hydro- In a particular form of the invention,

desulfurization. the naphtha feed is first combined with reformate previously produced, and the mixture subjected to the separation step, thereby removing aromatics which may be contained in the feed prior to subjecting the remainder to reforming and, likewise, increasing the elliciency of the separation step by decreasing the percentage of aromatics in the total fraction subjected to the separation. Ina specific form of the invention, low-boiling, predominately isoparafiinic hydrocarbons are removed by fractionation from the reformate prior to the separation step and are combined with the aromatic concentrate to produce a mixture of increased value in gasoline blending.

The invention may be more readily understood by reference to the drawing which is a diagrammatic flow diahave created a need for gasoline having a research octane number substantially above 90 (before the addition of tetra-ethyl lead or other anti-knock compound) and preferably above 96. To meet this requirement by catalytic reforming processes now in use, it is necessary to increase the severity of operating conditions to an extent that a substantial amount of hydro-cracking occurs with concomitant decrease in naphtha yield, increased equipment and operating cost to regenerate the catalyst (by burning off the carbon formed) and increased cost for a suitable catalyst capable of tolerating frequent regenera tion without a prohibitive amount of deterioration.

In accordance with the present invention, by the use of certain separation processes in combination with catalytic reforming under mild conditions, a higher yield of usable components for a 96 to 98 (or higher) octane gasoline can be obtained, than can be produced by catalytic reforming alone under conditions severe enough to pro-, duce the same anti-knock quality.

Broadly, the invention comprises catalytically reforming a naphtha of low anti-knock quality, separating from the reformate a concentrate containing most of the aromatics therein, and returning the remaining predominately paraffinic portion of the reformate to the reforming step for further conversion. Concentration of the aromatics may be byany suitable process, such as for example, by use of silica gel; by extractive distillation in the presence of phenol, cresylic acids, sulfolanes or glycolwater mixtures; or by solvent extraction (e.g. with liquid sulfur dioxide). The low antiknock naphtha fed to the process may be a virgin naphtha or it may be a fraction gram of the process. Naphtha in line 1, together with raflinate in line 2, and recycle hydrogen in line 3 is charged-to catalytic reforming zone4, wherein the mixture of hydrocarbons and hydrogen is passed in the vapor phase through a bed of reforming catalyst at temperatures in excess of 800 F. and at conditions of pressure, time and hydrogen concentration, to convert a substantial amount of the paraflinic charge to aromatic hydrocarbons with concomitant isomerization of other parafiinic constituents and production of hydrogen and certain lowboiling hydrocarbons. As is well known to the art, increased time and temperature and reduced pressures in catalytic reforming tend to increase cracking reactions with resulting formation of larger quantities of normally gaseous hydrocarbons and carbon. In accordance with the present invention, the conditions in zone 4 are maintained sufliciently moderate to permit treatment of at least 30 barrels of naphtha per pound of catalyst (and preferably more) without regeneration or replacement of catalyst. While such conditions vary with the naphtha treated and with the particular catalyst used, those conversant with catalytic reforming can readily select suitable conditions.

The efiluent from the catalytic reforming zone 4, comprising hydrogen, normally gaseous hydrocarbons, and normally liquid aromatic and parafiinic hydrocarbons, is discharged through line 5 into fractionating zone 6 which includes suitable traps, stills, absorption equipment and the like to fractionate the effluent into (1) a hydrogen fraction containing upwards of about 70% hydrogen, shown as leaving zone 6 through line 7; (2) a gas fraction composed principally of the C to C hydrocarbons formed in zone 4, but which may also contain some hydrogen and any excess C not usable in the finished gasoline, shown as leaving through line 8; (3) a light hydrocarbon fraction (line 9) composed mainly of hydrocarbons boiling below about 200 F.; and (4) heavy hydrocarbons, boiling above about 200 R, which leave through line 10.

Part of the hydrogen fraction in line 7 is recycled to the reforming zone 4 through line 3 to maintain required ratio of hydrogen therein in accordance with known principles. If desired, such hydrogen fraction may be treated to remove hydrogen sulfide or other unwanted impurities prior to entry into zone 4. The remainder of the hydrogen fraction in line 7 is passed through line 11 for any desired disposal. Likewise, the gas fraction in line 8 is disposed of asv desired.

Due to the nature of catalytic reforming, the light hydrocarbons in line 9 contain high percentages of isoparaflins of very high anti-knock value. In a preferred form of the invention, these are passed directly to blending zone 12 to be included in the finished gasoline. However, if desired, any or all of the hydrocarbons in line 9 may be mixed with the heavy hydrocarbons in line 10 3 tobetrested therewith,ssillustratedinthe drawingby dotted line 13.

The heavy hydrocarbons in line 10, together with any desired hydrocarbons from line 9, are charged to extraction zone 14. In extraction zone 14, the hydrocarbons are separated into an extract (composed predominately of aromatic hydrocarbons, shown as leaving through line and raifinate (composed of predominately paraflinic hydrocarboons, shown as leaving through line 16). As indicated prior, any one of the various well-known methods for separating aromatic from parafiinic hydrocarbons may be used for the separation in extraction zone 14. Extraction with liquid sulfur dioxide has proven suitable, and' will be used elsewhere herein for illustration.

The extract in line 15 is passed to blending zone 12 where it is blended with light hydrocarbons from line 9 to form anti-knock gasoline shown as leaving zone 12 through line 17. If desired, ingredients from other sources may be added in zone 12 for augmenting the quantity, correcting the volatility, or further improving the octane number.

The rafiinate in line 16 is returned through line 2 to reforming zone 4 for further treatment. It is thus seen that the raffinate is treated to extinction, with the products of the process being a predominately aromatic gasoline and gas. Due to the repeated recycling of the rafiinate, portions thereof recycled several times may prove somewhat more refractory to catalytic reforming than the original charge. In such cases it may be desirable to charge the rafiinate first to an auxiliary reforming zone (indicated in the drawing as 18) prior to entering zone 4, thus giving the raflinate more reforming treatment than the naphtha charge. The conditions in the auxiliary zone 18 may be milder, the same as, or somewhat more severe than those in zone 4. The preliminary treatment of the ratlinate, such as in zone 18, is the subject of and claimed in copending application of Ammer and Viland, filed March 27, 1956, Serial No. 574,295.

In certain cases, particularly when the naphtha charged to the process contains appreciable quantities of antiknock constituents extractable by the method employed in zone 14, or when the aromatic content of the heavy hydrocarbons in line 10 is so high as to render diflicult the operations in zone 14, it may be desirable to introduce part or all of the fresh naphtha charge to zone 14 (as shown by dotted line 19) instead of through line 1. With this modification of the invention, the aromatics in the naphtha charge will pass directly to the finished gasoline without being subjected to reforming conditions, and the paraflinic portions of the naphtha charge will reduce the percentage of aromatics in the total charge to zone 14 facilitating separation in some instances.

To further illustrate the invention, the ,following examples of operations under typical conditions are presented:


reforming catalyst under mild (non-regenerative) conditions. Hydrogen to maintain desired hydrogen to hydrocarbon ratio during the reforming is obtained by recycling hydrogen produced during the reforming reaction. The efiiuent from the reforming is cooled and passed to a high pressure gas separator from which a hydrogen stream of about 90% purity is withdrawn, part of which stream supplies the recycle hydrogen and the remainder (representing the major part of the hydrogen produced by the reforming reaction) is diverted to other uses.

The liquid hydrocarbons from the high pressure separa'tor are stabilized at lower pressure to produce a gas stream composed of propane and lighter hydrocarbons,

' v 4 a butanes stream, and a debutanlzed reformate stream containing about 45% aromatic hydrocarbons. This reformate is extracted by countercurrent extraction with liquid sulfur dioxide at 25' F. to give 3,600 barrels per day of the recycle raflinate analyzing about 15% aromatics and an extract stream of 5,250 barrels per day of debutanized, highly aromatic blending stocks having a research octane number of 98, suitable for use as the major constituent of high anti-knock gasoline or for other blending purposes as desired (either with or without the addition of part or all of the butanes stream). Table 1 shows additional data relating to this example.

Table 1 Reformer operating conditions:

Reactor temperature, F. 900-910 Reactor pressure, p.s.i.g 500 Space velocity (ratio liquid volume of charge per hour to gross volume catalyst) 3.0 Hydrogen ratio, mol. Il /mol. H.C. 5.5 Catalyst life, days Reformer charge:

Fresh naphtha, bbls./day 6,400 Recycle raflinate, bbls./day 3,600

Total, bb1s./day 10,000

Reformer yields: I

Hydrogen fraction (net), M c.f./day 10,000 Dry gas fraction, M c.f./day 1,000 Butanes, bbls./day 600 Debutanized reformate, bbls./day 8,850 Extraction conditions:

Volume $0, per volume reformate 1.25 Temperature, F. 25 Extraction yields:

Raflinate, bbls./day 3,600 Extract, bbls./day 5,250

Overall processing yields:

Butanes, percent of fresh naptha charge 9.4

Extract, percent of fresh naphtha charge 82.0

Yield of blending components 91.4

Octane No. extract (ASTM D-908-53) 98+ Octane No. extract plus butanes 98+ The properties of the various stocks made in Example 1 are shown in Table 2.

Table 3 shows typical results obtained when treating the same fresh naphtha charge by reforming alone (a) at the same operating conditions as shown in Table l and (b) at operating conditions sufficiently sever to yield about 98 octane number debutamzed reformate.

Ten thousand barrels per'day of rafliuate, obtained from a later stage of the process, are catalytically reformed over the same type of platinum catalyst and with similar operating conditions as in Example 1. The effluent from the reforming is fractionated in a manner similar to Example 1 to obtain a hydrogen stream, a dry gas stream of propane and lighter hydrocarbons, a butancs stream, and a debutanized reformate stream. The debutanized reformate stream is further fractionated to remove a light out composed chiefly of (predominately isoparaflinic) pentanes and hexanes, leaving a 90% heavy cut containing the aromatic hydrocarbons produced in the reforming reaction.

The heavy cut, which may have a volume of about 8,000 barrels per day and may analyze about 50% aro matics, is combined with 8,000 barrels per day of fresh naphtha charge to the process. The fresh naphtha selected for this example is a 200 to 400 F. boiling range straight-run naphtha distilled from California crude and analyzing about aromatics. The mixture of heavy cut and fresh naphtha charge, now analyzing about 30 to 35% aromatics, is countercurrently extracted at F. with liquid sulfur dioxide to give 10,000 barrels per day of recycle ratfinate (constituting the charge to the reformer) and 6,000 barrels per day of blending stock having an aromatic content of about 70%. This blending stock may be blended as desired wtih gasoline components from other sources to enhance their anti-knock value. However, preferably, this blending stock is combined with the 10% light out previously mentioned :to obtain a maximum yield of high octane gasoline, to which is added suflicient of the butanes stream to meet seasonal volatility requirements.

Table 4 shows additional data relating to th: example.

Reformer charge: Recycle nflinate, bbL/day 10,000 Reformer yields:

Hydrogen fraction (net) M. c.f./day 9,500

Dry gas fraction, M c.f./dsy 950 Butanes, bbL/day 600 Light reformate cut, bblJday 850 Heavy reformate cut, bbL/day 8,000 Extraction eonditiom:

Volume SO, per volume hydrocarbons 1.25

6 Extraction charge:

Fresh naphtha charge, bbl./day 8,000 "Heavy reformate out, bblJday 8,000

Total 16,000

Extraction yields:

Ralfinate, bbl./day 10,000 Extract, bbL/day 6,000

Overall processing yields: I

Light reformate cut, percent fresh naphtha charge 10.6 Extract, percent of fresh naphtha charge 75.0 Butane-free components, percent 85.6 Butanes, percent of fresh naphtha charge 7.5

Total blending components 93.1

Octane No. extract 98+ Octane No. extract plus light out 97 Octane No. extract plus light out plus butanes 98 As illustrated in the foregoing examples, it is evident that greatly increased yields of high octane gasoline components may be made by the combination of aromatic concentration with catalytic reforming, over yields obtainable by catalytic reforming alone. The examples, however, are given to illustrate the processing steps and yields obtainable, and are not to be considered as limiting the invention in its broadest scope. As aforementioned, the invention, broadly, contemplates the use of any catalytic reforming method conducted in the presence of hydrogen wherein substantial quantities of aromatics are produced, and any method for concentrating the aromatics produced to obtain a predominately aromatic and a predominately paraflinic fraction. I

I claim:

A process for producing highly aromatic anti-knock gasoline components, which comprises: passing a continuous stream of predominately parafiinic hydrocarbon naphtha vapors and hydrogen through a bed of reformingcatalyst under conditions to convert a substantial portion of said naphtha to aromatic hydrocarbons and additional hydrogen without substantial deposition of carbon on said catalyst, fractionating the resulting productsinto a gas fraction, a light hydrocarbon fraction composed predominately of isoparaifinic hydrocarbons of from 4 to 6 carbon atoms and boiling below about 200' F. and a heavy hydrocarbon reformate fraction boiling above, 200' F., separating said gas fraction'and said light hydrocarbon fraction from said heavy hydrocarbon reformate fraction, combining said latter reformate fraction with fresh, predominately paraflinic naphtha of the type initially charged to the process, solvent extracting said reformate fraction-fresh naphtha mixture to produce a predominately aromatic gasoline extract and a predominately heavy parafiinic raflinte, recycling the raflinate to said catalyst bed as part of said hydrocarbon naphtha w vapor feed, and blending at least part of said light hydro- Tcmpersture, F. 25 A References Cited ln-the file of this UNITED STATES PATENTS 5 2,125,714 Fulton Aug. 2, 1938 2,409,695 Laughlin Oct. 22, 1946 2,479,110 Haensel Aug. 16, 1949 2,593,561 Herbst et a1. Apr. 22, 1952 2,736,684 Tampoll Feb. 28, 1956 10 2,768,126 Haensel et a1. Oct. 23. 1956 carbon fraction with said aromatic gasoline extract.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2125714 *Oct 26, 1935Aug 2, 1938Standard Oil Dev CoNaphtha reforming
US2409695 *Jan 30, 1943Oct 22, 1946Standard Oil Dev CoMethod for improving aviation fuels
US2479110 *Nov 28, 1947Aug 16, 1949Universal Oil Prod CoProcess of reforming a gasoline with an alumina-platinum-halogen catalyst
US2593561 *Sep 4, 1948Apr 22, 1952Standard Oil Dev CoMethod of preparing rich-mixture aviation fuel
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Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2933445 *Apr 8, 1955Apr 19, 1960Sun Oil CoCatalytic reforming process employing a blend of selected hydrocarbon fractions
US2938853 *Mar 27, 1956May 31, 1960Tidewater Oil CompanyManufacture of antiknock gasoline
US2970101 *May 7, 1958Jan 31, 1961American Oil CoPreparation of high octane number motor fuel blending stocks
US2976231 *Jun 22, 1959Mar 21, 1961Universal Oil Prod CoProduction of an aromatic fuel by solvent extraction of the reformate fractions
US2981675 *Dec 23, 1957Apr 25, 1961Exxon Research Engineering CoSubsequent treatment of a naphtha reformate to obtain a high octane gasoline
US3070637 *Aug 3, 1959Dec 25, 1962Sun Oil CoPreparation of benzene and toluene
US3124524 *Jun 1, 1959Mar 10, 1964 Distillation
US8889943 *Feb 2, 2007Nov 18, 2014William George RhodeyProcess and system for extraction of a feedstock
US20070129590 *Feb 2, 2007Jun 7, 2007Rhodey William GProcess and system for extraction of a feedstock
USRE33323 *Jun 10, 1988Sep 4, 1990Exxon Research & Engineering CompanyReforming process for enhanced benzene yield
U.S. Classification208/96, 208/100, 208/188, 585/413, 585/752, 208/138
International ClassificationC10L1/00, C10G61/06, C10G61/00, C10L1/06
Cooperative ClassificationC10G61/06, C10L1/06
European ClassificationC10L1/06, C10G61/06